WO2000055282A1 - Cavitation enhanced liquid atomization - Google Patents
Cavitation enhanced liquid atomization Download PDFInfo
- Publication number
- WO2000055282A1 WO2000055282A1 PCT/US2000/005034 US0005034W WO0055282A1 WO 2000055282 A1 WO2000055282 A1 WO 2000055282A1 US 0005034 W US0005034 W US 0005034W WO 0055282 A1 WO0055282 A1 WO 0055282A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- liquid
- atomizing
- fluid
- process according
- pressure
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/008—Processes for carrying out reactions under cavitation conditions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
Definitions
- the invention relates to cavitation enhanced liquid atomization. More particularly, the invention relates to atomizing a fluid comprising a solution of the liquid to be atomized and a lower boiling cavitation liquid, by contacting the fluid under pressure and while flowing, with a pressure reducing means to reduce the fluid pressure and thereby produce nucleation and growth of bubbles comprising vapor of the cavitation liquid in the fluid, at a temperature below the bubble point of the solution, and then passing the fluid through an atomizing means into a lower pressure atomizing zone. Bubble nucleation is induced upstream of the atomizing means. This is useful for atomizing a hot FCC feed oil into a catalytic cracking reaction zone, using a lower boiling hydrocarbon as the cavitation liquid.
- Fluid atomization is well known and used in a wide variety of applications and processes. These include, for example, aerosol sprays, the application of pesticides and coatings, spray drying, humidification, mixing, air conditioning, and chemical and petroleum refinery processes.
- a fluid under pressure with or without the assistance of an atomizing gas, is forced through a pressure reducing orifice in an atomization nozzle.
- Atomization occurs as the fluid passes through the orifice and into the lower pressure zone downstream.
- the degree of atomization is determined by the orifice size, the pressure drop across the orifice, fluid density, viscosity, and surface tension, etc., as is known. Atomization is increased and the droplet size is decreased, with decreasing orifice size and increasing pressure drop.
- FCC fluidized catalytic cracking
- fluid cat cracking as it is also called
- FCC is an established and widely used process in the petroleum refining industry, primarily for converting high boiling petroleum oils to more valuable lower boiling products, including gasoline and middle distillates such as kerosene, jet and diesel fuel, and heating oil.
- the preheated oil feed is mixed with steam or a low molecular weight (e.g., C 4 .) gas under pressure, to form a two phase, gas and liquid fluid.
- steam or a low molecular weight e.g., C 4 .
- This fluid is passed through a pressure-reducing orifice into a lower pressure atomization zone, in which the gas expands and the oil is atomized, and brought into contact with a particulate, hot cracking catalyst.
- the atomization is effected primarily by the shearing action between the gas and liquid phases, as the fluid passes through the orifice and into the lower pressure atomization zone.
- the FCC riser comprises both the feed atomization zone and the cat cracking zone.
- Steam is more often used than a light hydrocarbon gas, to reduce the vapor loading on the on the gas compression facilities and the downstream products fractionation. However, the use of steam produces sour water, which enhances corrosion. Sour water is also environmentally unfriendly and must therefore be treated before disposal. There is a need therefore, for a process that either reduces or eliminates the amount of steam or low molecular weight gas atomizing agents.
- the invention relates to a liquid atomizing process in which a fluid comprising a solution of the liquid to be atomized and a lower boiling cavitation liquid, is contacted under pressure and while flowing, with a pressure reducing means to reduce the fluid pressure and thereby produce nucleation of bubbles comprising the cavitation liquid vapor in the fluid, at a temperature below the bubble point of the solution, and then passing the fluid through an atomizing means into a lower pressure atomizing zone.
- the cavitation bubbles comprise vapor of the cavitation liquid. Nucleation of the cavitation bubbles produces a two-phase fluid comprising the vapor bubbles and the liquid solution.
- Passing the so-formed two-phase fluid through the atomizing means also produces shear between the vapor (the cavitation bubbles) and liquid phases, which increases the surface area of the liquid, as reflected in the formation of ligaments, membranes, smaller globules, etc.
- the atomization produces a spray of liquid droplets into the lower pressure atomizing zone. This is explained in detail below.
- pressure is meant a low pressure reducing means, such as one or more static mixers in the fluid line upstream of the atomizing means.
- low pressure is meant that the static mixer(s) or other pressure reducing means produces, in the flowing fluid, a pressure drop less than 50 psi, preferably less than 15 psi and more preferably no greater than 5 psi upstream of the atomizing means, with a typical pressure drop ranging from 1 to 5 psi.
- Cavitation is a phenomena in which a pressure drop induces bubble formation in a liquid, at a temperature below the bubble point of the liquid.
- cavitation occurs by reducing the pressure, while maintaining a constant temperature. This is in contrast to boiling enhanced atomization, in which bubble nucleation is induced by increasing the temperature of the fluid above the bubble point, while maintaining the pressure constant.
- the cavitation liquid is soluble in the liquid to be atomized at the process conditions and either has a lower boiling point than the liquid to be atomized or contains sufficient material boiling below the boiling range of the liquid to be atomized, to form bubbles which grow and expand for the atomization. Typically this means that at least 0.5 wt. %, preferably at least 1.0 wt. % and more preferably greater than 1.0 wt. % of the cavitating liquid will be vaporized during the initial bubble formation and subsequent atomization of the liquid to be atomized.
- the fluid produced by mixing the cavitating liquid with the liquid to be atomized is preferably a single phase liquid mixture or solution, as opposed to two liquid phases or an emulsion.
- the process of the invention is useful for atomizing a wide variety of liquids, including chemical and refinery process liquids, such as atomizing a hot FCC feed oil into a cat cracking reaction zone, using a lower boiling hydrocarbon as the cavitation liquid.
- chemical and refinery process liquids such as atomizing a hot FCC feed oil into a cat cracking reaction zone, using a lower boiling hydrocarbon as the cavitation liquid.
- a two- phase mixture of an FFC oil feed liquid and an atomizing agent comprising steam flows through a feed injector which terminates at its downstream end in an atomizing means comprising an atomizing orifice.
- the downstream side of the atomizing orifice opens downstream into a spray distributor, as is known.
- a cavitating fluid comprising one or more lower boiling hydrocarbons or lower boiling hydrocarbon fractions
- the hot oil either upstream of the injector or within the injector, to form the fluid solution which, at this point, is a liquid.
- the injector typically comprises one or more conduits for flowing one or more liquids through and terminates at its downstream end in an atomizing means.
- the liquid solution of FCC feed oil and the one or more cavitating liquids is maintained at a pressure and temperature, such that cavitation preferably does not occur until the flowing fluid contacts one or more pressure reducing means in the injector, to produce a pressure drop in the fluid and thereby induce nucleation and growth of bubbles comprising the vapor of the cavitating fluid(s) dissolved in the hot oil.
- This bubble nucleating pressure drop may be as much as one-third of the pressure drop of the fluid through the injector and into the FCC cat cracking zone, as an oil spray comprising droplets of the atomized oil.
- the pressure drop inducing means is located upstream of the atomizing means. Such means will preferably include one or more static mixing means located in the fluid conduit upstream of the atomizing means.
- a plurality of such means may be located in the fluid conduit so that the flowing fluid successively contacts more than one such means as it flows downstream to the atomizing means.
- This embodiment will produce bubble nucleation and growth in the oil feed as it approaches the atomizing means.
- the fluid pressure upstream of the pressure drop means is preferably maintained sufficiently high to prevent bubble nucleation and this means a pressure greater than the vapor pressure or bubble nucleation pressure of the solution at the design temperature.
- the pressure in the atomizing zone is greater than the vapor pressure of the liquid to be atomized, but lower than the vapor pressure of the cavitating fluid and preferably sufficiently lower to further promote and ensure rapid vaporization or flashing of the cavitating liquid to assist in forming the spray of liquid droplets.
- the atomizing orifice may comprise the upstream entrance of a controlled expansion atomizing zone, such as the fan-shaped distributor of the type disclosed in U.S. patent 5,173,175 which provides a fan- shaped spray of the atomized liquid into the FCC cat cracking reaction zone.
- the orifice may also comprise a shaped slot at the end of a conduit, for providing a more or less fan-shaped spray as disclosed, for example, in U.S. patents 4,784,328 and 5,289,976. Other embodiments will be explained in detail below.
- the process of the invention is useful for atomizing any liquid, including aqueous liquids as well as hydrocarbonaceous liquids.
- the cavitating liquid may be acetone, methanol and the like.
- hydrocarbon gas e.g., C
- the invention comprises a fluid cat cracking process which comprises the steps of:
- the lower boiling hydrocarbons produced by the cracking reaction are separated from the spent catalyst particles, in a separation zone, are recovered and then typically sent to further processing, including fractionation.
- the cracking - 7 - reaction also produces spent catalyst particles, which contain strippable hydrocarbons and coke, as is known.
- the spent catalyst particles are stripped in a stripping zone, to remove the strippable hydrocarbons to produce stripped, coked catalyst particles.
- the stripped, coked catalyst particles are passed into a regeneration zone, in which they are contacted with oxygen, at conditions effective to burn off the coke and produce the hot, regenerated catalyst particles, which are then passed back up into the reaction zone.
- the reaction zone of an FCC cat cracking process usually comprises a riser and is known as a riser reaction zone.
- FIGS 1(a) and 1(b) are simplified side and plan view schematic illustrations of an FCC feed injection unit useful in the practice of the invention.
- Figure 2 is a graph of vapor pressure as a function of temperature for saturated hydrocarbon cavitating fluids.
- the fluid passing through the atomizing means which typically comprises an atomizing orifice, having a cross-sectional area perpendicular to the fluid flow direction smaller that that of the fluid flow conduit upstream, as further described below, is a two-phase fluid comprising a gas phase and a liquid phase.
- the gas phase comprises cavitation liquid vapor and the liquid phase comprises a solution of the cavitation liquid and the liquid to be atomized.
- the two-phase fluid passing through the atomizing means may be gas-continuous or liquid-continuous, or it may be a bubbly froth, in which it may not be known with certainty if one or both phases are continuous. This may be further understood with reference to, for example, an open cell sponge and a closed cell sponge.
- Sponges typically have a 1 : 1 volumetric ratio of air to solid.
- An open cell sponge is both gas (air) and solid continuous, while a closed cell sponge is solid continuous and contains discrete (dispersed) gas cells.
- the solid can be said to be in the form of membranes and ligaments (such as may exist in a two-phase gas-liquid froth or foam).
- the gas can be envisioned as in the form of a dispersion of discrete gas globules in the solid. Some sponges fall in-between the two, as do some two- phase fluids comprising a gas phase and a liquid phase.
- the fluid passed through the atomizing means, to form the spray of oil droplets comprise mostly cavitating fluid vapor on a volumetric basis (e.g., a volumetric vapor to liquid ratio of at least 2: 1).
- a single phase fluid (e.g., liquid) passed through the nozzle will have its kinetic energy increased.
- the vapor velocity may be increased relative to the velocity of the liquid phase, (i) in mixing zones between the bubble nucleation and pressure drop means, (ii) when the fluid passes through an atomizing orifice of smaller cross-section, pe ⁇ endicular to the fluid flow direction, than the fluid conduit means upstream of the orifice (a pressure-reducing orifice).
- This velocity differential between the vapor and liquid phases is believed to result in ligamentation of the liquid, particularly with a viscous liquid, such as a hot FCC feed oil.
- ligamentation is meant that the liquid forms elongated globules or ligaments which are sometimes referred to as rivulets.
- the atomizing zone is at a lower pressure than the pressure upstream of the atomizing orifice. Consequently, the vapor in the fluid passing through the atomizing orifice rapidly expands, thereby further shearing, squeezing and dispersing the liquid ligaments and/or droplets into the atomizing zone. Any ligaments typically break into two or more droplets during the atomization.
- an FCC feed injection unit 10 comprises a hollow, liquid feed conduit 12, through which a hot, liquid FCC oil feed is passed from an upstream source.
- a cavitation liquid comprising a lower boiling hydrocarbon liquid is passed down into the conduit 12 via linel4, which intersects the conduit at the tee joint, as shown.
- the cavitation liquid is injected into the flowing hot oil, with it mixes, to form a liquid solution comprising both liquids, in the vicinity of zone 16.
- This mixing to form the fluid solution is shown here as occurring in the fluid conduit upstream of the pressure drop means 18, for the purposes of illustrating one embodiment of the invention. However, such mixing may be achieved further upstream and even outside of the feed injector, if desired.
- the pressure in the conduit is sufficient to maintain the cavitating fluid in the liquid state, so that the so-formed mixture is essentially all liquid.
- This fluid mixture progresses downstream (from left to right) and passes through a low pressure drop static mixer 18, which induces bubble nucleation.
- the so- formed fluid mixture having nucleated microbubbles continues downstream in the conduit to an atomizing orifice 22, smaller in cross-section than that of the conduit.
- cross-section is meant the cross-sectional area of the conduit ( ⁇ r 2 for a cylindrical conduit) and the cross-sectional area of the atomizing orifice pe ⁇ endicular to the fluid flow direction.
- the wall of the conduit terminates into the orifice by means of an arcuate or curved surface, 20, which converges the flowing fluid stream into the atomizing orifice with minimal coalescence, which might otherwise occur if the fluid impinged onto the end of the conduit.
- the downstream side of atomizing orifice 20, is contiguous with, and opens into a hollow, fan-shaped spray distributor 26 containing cavity 24.
- Cavity 24 comprises the controlled expansion zone, to create a fan-shaped spray of the atomized feed droplets.
- the pressure downstream of the atomizing orifice is sufficiently lower than the pressure on the upstream side in the conduit, for the cavitating fluid to flash or rapidly vaporize to atomize the FCC feed liquid into droplets in the controlled expansion atomization zone 24.
- An important and essential feature of the invention resides in nucleating, in the liquid to be atomized, bubbles comprising cavitating fluid vapor by pressure drop means, and preferably upstream of the atomizing orifice. More preferably it will be advantageous to permit the nucleated bubbles to grow by, i.e., additional pressure drop inducing means upstream of the atomizing means.
- the pressure drop means preferably comprises one or more static mixers, to provide the desired bubble nucleation with a minimal pressure drop. If the two liquids, the feed and cavitating liquid, are merely mixed together and then passed through an atomizing means without bubble nucleation, the bubble expansion and vaporization will be slower and the desired degree of atomization of the feed liquid will not be achieved.
- the pressure drop across one or more static mixers upstream of the atomizing means and concomitant agitation of the so-formed bubble containing solution initiates bubble nucleation and preferably bubble nucleation and growth, so that expansion of the bubble vapor is much more rapid across the atomizing orifice, and feed atomization is therefore enhanced.
- foaming either does not occur or occurs slowly. If the soda is agitated before opening, rapid and violent foaming occurs when the bottle is opened and the pressure is released. Shaking of the bottle allows the soda to be sprayed out as a spray or mist, due to the rapid bubble growth across the opening where the pressure reduction occurs.
- the reduction in pressure and agitation produced by the upstream mixer causes bubble nucleation just as shaking the soda, and the resulting fine atomization of the feed can be accomplished by the subsequent depressurizing and the cavitating mechanism described, rather than by the two phase shearing, as with conventional atomization nozzles.
- the bubble nucleating means is preferably designed and/or selected to produce the smallest pressure drop necessary to vaporize a small fraction, which is less than half and preferably less than one-third, of the cavitating liquid to provide bubble nucleation, with the major portion of the pressure drop occurring across the atomization nozzle, to generate the atomized spray.
- Cat cracker feeds used in FCC processes typically include gas oils, which are high boiling, non-residual oils, such as a vacuum gas oil (NGO), a straight run (atmospheric) gas oil, a light cat cracker oil (LCCO) and coker gas oils. These oils have an initial boiling point typically above about 450°F (232°C), and more commonly above about 662°F (350°C), with end points up to about 1 150°F (621°C), as well as straight run or atmospheric gas oils and coker gas oils.
- gas oils which are high boiling, non-residual oils, such as a vacuum gas oil (NGO), a straight run (atmospheric) gas oil, a light cat cracker oil (LCCO) and coker gas oils.
- NGO vacuum gas oil
- LCCO light cat cracker oil
- coker gas oils have an initial boiling point typically above about 450°F (232°C), and more commonly above about 662°F (350°C), with end points up to about
- one or more heavy feeds having an end boiling point above 1050°F may be blended in with the cat cracker feed.
- Such heavy feeds include, for example, whole and reduced crudes, resids or residua from atmospheric and vacuum distillation of crude oil, asphalts and asphaltenes, tar oils and cycle oils from thermal cracking of heavy petroleum oils, tar sand oil shale oil, coal derived liquids, syncrudes and the like. These may be present in the cracker feed in an amount of from about 2 to 50 volume % of the blend, and more typically from about 5 to 30 volume %.
- feeds typically contain too high a content of undesirable components, such as aromatics and compounds containing heteroatoms, particularly sulfur and nitrogen. Consequently, these feeds are often treated or upgraded to reduce the amount of undesirable compounds by processes, such as hydrotreating, solvent extraction, solid absorbents such as molecular sieves and the like, as is known.
- Typical cat cracking conditions in an FCC process include a temperature of from about 800- 1200°F (427-648°C), preferably 850-1 150°F (454-621°C) and still more preferably 900-1 150°F (482-621°C), a pressure between about 5-60 psig, preferably 5-40 psig with feed/catalyst contact times between about 0.5-15 seconds, preferably about 1-5 seconds, and with a catalyst to feed ratio of about 0.5-10 and preferably 2-8.
- the FCC feed is preheated to a temperature of not more than 850°F, preferably no greater than 800°F and typically within the range of from about 600-800°F.
- the lower boiling cavitating fluid must be soluble in, and compatible with, the liquid to be atomized and with any upstream processes conditions for each specific application.
- a vapor pressure graph for hydrocarbons shown in Figure 2.
- this graph is a simplified version of the one disclosed by Maxwell and Bonnell, in an article titled Derivation and Precision of a New Vapor Pressure Correlation for Petroleum Hydrocarbons, which appeared in Industrial and Engineering Chemistry, v.49, pages 1 187- 1 196
- the pressure in the fluid conduit upstream of the atomizing orifice is assumed to be 7 atmospheres and the pressure on the downstream side of the orifice, in the atomization zone, is assumed to be 3 atmospheres.
- the cavitating liquid For an upstream temperature of 750-800°F, the cavitating liquid must be a liquid at 7 atmospheres and a vapor at 3 atmospheres. This suggests that a normal boiling point between 600 and 650°F is required for the cavitating liquid, although the nominal boiling point for this cavitating liquid would be adjusted based on the planned treat rate, as well as considering the boiling range and miscibility of the fluid with the process feed.
- the cavitating liquid could be a distillate fraction produced from the FCC process or it could be obtained from another source.
- a blend of 1-5 wt. % of the distillate, based on the FCC feed, will generate a two phase volume expansion of 1.7-4.3 times the liquid feed volume, with a temperature drop of between 1-7 degrees, from an adiabatic flash. If the upstream conditions are changed to 7 atmospheres and 400-450°F, the required boiling range for the cavitating fluid is approximately 290-315°F.
- an optimum cavitating fluid boiling range can be defined.
- Droplet images of the sprays were taken with a CCD camera.
- the orifice opened into the heated air chamber at the downstream side.
- the temperature in the chamber was identical to the liquid temperature, to minimize fluid temperature changes due to the atomization and evaporation.
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU33827/00A AU763579B2 (en) | 1999-03-18 | 2000-02-25 | Cavitation enhanced liquid atomization |
EP00912027A EP1171548A4 (en) | 1999-03-18 | 2000-02-25 | Cavitation enhanced liquid atomization |
CA002365531A CA2365531A1 (en) | 1999-03-18 | 2000-02-25 | Cavitation enhanced liquid atomization |
JP2000605701A JP2002538963A (en) | 1999-03-18 | 2000-02-25 | Atomizing liquid with enhanced cavitation |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US09/271,707 US6171476B1 (en) | 1999-03-18 | 1999-03-18 | Cavitation enhanced liquid atomization |
US09/271,707 | 1999-03-18 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000055282A1 true WO2000055282A1 (en) | 2000-09-21 |
Family
ID=23036726
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2000/005034 WO2000055282A1 (en) | 1999-03-18 | 2000-02-25 | Cavitation enhanced liquid atomization |
Country Status (7)
Country | Link |
---|---|
US (1) | US6171476B1 (en) |
EP (1) | EP1171548A4 (en) |
JP (1) | JP2002538963A (en) |
CN (1) | CN1344309A (en) |
AU (1) | AU763579B2 (en) |
CA (1) | CA2365531A1 (en) |
WO (1) | WO2000055282A1 (en) |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6783662B2 (en) * | 1999-03-18 | 2004-08-31 | Exxonmobil Research And Engineering Company | Cavitation enhanced liquid atomization |
CN1370215A (en) | 1999-08-26 | 2002-09-18 | 埃克森美孚研究工程公司 | Superheating atomizing steam with hot FFC feed oil |
US7383828B2 (en) * | 2004-06-24 | 2008-06-10 | Emission & Power Solutions, Inc. | Method and apparatus for use in enhancing fuels |
US7428896B2 (en) * | 2004-06-24 | 2008-09-30 | Emission & Power Solutions, Inc. | Method and apparatus for use in enhancing fuels |
CN105664803A (en) * | 2008-12-29 | 2016-06-15 | 巴塞尔聚烯烃意大利有限责任公司 | Process for feeding a catalyst in a polymerization reactor |
FR3077510B1 (en) * | 2018-02-08 | 2022-07-22 | Total Raffinage Chimie | CHARGE INJECTION DEVICE OF AN FCC UNIT WHOSE CROSS SECTION IS LOCALLY INCREASED. |
WO2021138367A1 (en) * | 2020-01-02 | 2021-07-08 | Clearrefining Technologies, Llc | System and method for making a kerosene fuel product |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4784328A (en) * | 1983-10-14 | 1988-11-15 | Phillips Petroleum Company | Nozzle assembly |
US5173175A (en) * | 1990-04-27 | 1992-12-22 | Exxon Research And Engineering Company | Fcc feed injector |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5289976A (en) | 1991-12-13 | 1994-03-01 | Mobil Oil Corporation | Heavy hydrocarbon feed atomization |
US6003789A (en) | 1997-12-15 | 1999-12-21 | Aec Oil Sands, L.P. | Nozzle for atomizing liquid in two phase flow |
US6142457A (en) * | 1998-01-30 | 2000-11-07 | Mobil Oil Corporation | Atomizing feed nozzle |
-
1999
- 1999-03-18 US US09/271,707 patent/US6171476B1/en not_active Expired - Fee Related
-
2000
- 2000-02-25 JP JP2000605701A patent/JP2002538963A/en active Pending
- 2000-02-25 WO PCT/US2000/005034 patent/WO2000055282A1/en active Search and Examination
- 2000-02-25 CA CA002365531A patent/CA2365531A1/en not_active Abandoned
- 2000-02-25 EP EP00912027A patent/EP1171548A4/en not_active Withdrawn
- 2000-02-25 CN CN00805199.2A patent/CN1344309A/en active Pending
- 2000-02-25 AU AU33827/00A patent/AU763579B2/en not_active Ceased
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4784328A (en) * | 1983-10-14 | 1988-11-15 | Phillips Petroleum Company | Nozzle assembly |
US5173175A (en) * | 1990-04-27 | 1992-12-22 | Exxon Research And Engineering Company | Fcc feed injector |
Non-Patent Citations (1)
Title |
---|
See also references of EP1171548A4 * |
Also Published As
Publication number | Publication date |
---|---|
US6171476B1 (en) | 2001-01-09 |
CA2365531A1 (en) | 2000-09-21 |
EP1171548A1 (en) | 2002-01-16 |
AU3382700A (en) | 2000-10-04 |
CN1344309A (en) | 2002-04-10 |
EP1171548A4 (en) | 2002-11-06 |
AU763579B2 (en) | 2003-07-24 |
JP2002538963A (en) | 2002-11-19 |
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